CN103031141B - A kind of method removing mercaptan in oils - Google Patents
A kind of method removing mercaptan in oils Download PDFInfo
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- CN103031141B CN103031141B CN201110290862.9A CN201110290862A CN103031141B CN 103031141 B CN103031141 B CN 103031141B CN 201110290862 A CN201110290862 A CN 201110290862A CN 103031141 B CN103031141 B CN 103031141B
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Abstract
The invention provides a kind of method removing mercaptan in oils, comprising: activator, phthalocyanine catalyst are mixed in reaction vessel with oils, injection oxygen or air carry out contact reacts, collect product; Described activator is the mixture of hydrazine class compound and solvent, described phthalocyanine catalyst be selected from that metal phthalocyanine, sulfonated metal phthalocyanine derivative and metal gather in phthalocyanine compound one or more.The inventive method mercaptan removal is effective, does not cause secondary pollution to gasoline, without the discharge of waste lye, and has simple to operate, that cost of investment is low advantage.
Description
Technical field
The present invention relates to a kind of method removing mercaptan in oils, be particularly useful for pretreatment process light FCC gasoline raw material of etherification being carried out to mercaptan removal.
Background technology
Mercaptan is prevalent in oils, and too much mercaptan can produce foul smell, and affects oil quality, makes the destabilization component in oil product be oxidized, be overlapped into jelly.Mercaptan meeting corroding metal, and the corrodibility of elementary sulfur can be made to aggravate, mercaptan also affects the susceptibility of oil product to portions additive.Special in the preprocessing process of raw material of etherification, mercaptan will cause diolefine selective hydrogenation catalyst poisoning.Therefore, the mercaptan in petroleum products must remove.The industrial mercaptan removal method generally adopted is catalytic oxidation at present, the method utilizes a kind of catalyzer to make the mercaptan in oil product be oxidized to disulphide under aqueous alkali (sodium hydroxide solution) and air existent condition, and its chemical equation is: RSH+1/2O
2→ RSSR+H
2o, this method is also referred to as Merox method.It is large to there is alkali lye discharge in traditional Merox method, and technical process is tediously long, complicated operation, light-end products may carry the problems such as sodium ion.Along with the appearance of environmental regulation and the enhancing of environmental consciousness, there is the deodour method in a large number Merox method improved.
CN1456637A discloses a kind of solid alkali that adopts and carries out the method for deep desulfuration to light-end products, oil product is first through solid alkali cleaning or liquid alkali cleaning, solid alkali cleaning is that special solid alkali is loaded on fixed bed, liquid alkali cleaning is that sodium hydroxide solution is placed in container tank, afterwards and activator mix, enter deodorizing tower deodorization, finally by gas-liquid separation and sand filtration deodorization oil product.The method, compared with deodorizing technology at that time, can reduce by the waste lye quantity discharged of 50%, high-efficiency activated dose of the s-generation multiple active components that its activator used is developed for University of Petroleum, but the structure of unexposed activator.CN1194294A discloses a kind of technique of aviation kerosene alkali-free sweetening, by after aviation kerosene and activator mix, mercaptan removal is carried out by beds together with air, activator used is ZX-1827 (its structure is unexposed in application documents), used catalyst is sulfonated phthalocyanine cobalt, and the preparation method of beds is: make the sodium hydroxide solution containing catalyzer flow through the reactor that gac is housed, iterative cycles, soak more than 5 hours, exit alkali lye.CN1420157A proposes a kind of method removing non-leaded gasoline medium sulphide content under without sodium hydroxide condition, specific practice will be stripped of hydrogen sulfide completely and the catalytic gasoline of transform portion mercaptan, air and activator have been sent into be equipped with in the fixed-bed reactor of catalyzer and carried out sweetening reaction, catalyzer is the poly-Cobalt Phthalocyanine of load on pressed active carbon or sulfonated phthalocyanine cobalt, and activator is weak ammonia liquor.CN1048543A discloses a kind of mercaptan removal method containing mercaptan hydrocarbon-fraction, it under air and ammonium hydroxide exist with a kind of quaternary ammonium compound aqueous solution, hydrocarbon-fraction is contacted, the aqueous solution contains methyl alcohol, and the carrier of metal phthalocyanine catalytic composition is gac, aluminum oxide, silicon oxide etc.CN1952051A proposes a kind of for catalytic gasoline fixed bed alkaline-free sweetening method; mainly before catalytically cracked gasoline enters mercaptan oxidation tower, add alcohols, activator that guanidine class mixes and mercaptan-eliminating catalyst; because guanidine class is easy and Macromolecule mercaptan complexing in gasoline; increase the contact surface of mercaptan and catalyzer; mercaptan in catalytically cracked gasoline is removed, and the method mercaptan removal is effective, and cost is low; significantly can reduce waste lye discharge, protect environment.
US4923596 discloses a kind of sour hydrocarbon fraction deodorizing technology containing mercaptan, is characterised in that: hydrocarbon-fraction is contacted with the alkaline solution of tensio-active agent quaternary ammonium compound with containing metal intercalating agent in the presence of an oxidizer and carries out sweetening reaction.Described oxygenant is oxygen or air.Metal cheating agents is Cobalt Phthalocyanine, exists with the concentration of 0.1 ~ 2000ppm.Quaternary ammonium compound is quaternary ammonium hydroxide.Alkaline solution to be massfraction be 0.1% ~ 25% aqueous sodium hydroxide solution.US4908122 discloses a kind of deodour method of the sour hydrocarbon fraction containing mercaptan, the method make mercaptan removal raw material under the existence of oxygen or air with a kind of catalytic composition and the activating agent that effectively mercaptan oxidation can be become disulphide.Catalytic composition is the phthalocyanine cobalt catalyst of load on absorbent charcoal carrier, and activator is ammonium hydroxide and the quaternary ammonium salt except oxyhydroxide, and quaternary ammonium salt is the chlorate of quaternary ammonium, and concentration is 0.05 ~ 500ppm, and the amount that activator adds is 0.1 ~ 200ppm.
Above-mentioned patent never Merox mercaptan process faced by Tongfang is improved, and decreases the discharge of waste lye, but fundamentally solves the problem of waste lye discharge.
Summary of the invention
The object of the present invention is to provide a kind of method removing mercaptan in oils, the method is without the discharge of waste lye.
Remove a method for mercaptan in oils, comprising:
Under the existence of phthalocyanine catalyst and oxygen or air, by activator and oils contact reacts in the reactor, collect product; Described activator is the mixture of hydrazine class compound and solvent.
Specifically, hydrazine class compound described in activator is selected from the alkyl derivative of hydrazine, hydrazine hydrate and/or hydrazine, preferred hydrazine hydrate, C1 ~ C5 alkyl hydrazine and/or C1 ~ C5 alkyl substituted benzene hydrazine, most preferable hydrazine, ethyl hydrazine, propyl group hydrazine, butyl hydrazine, amyl group hydrazine, unsymmetrical dimethyl hydrazine, hydrazine hydrate, a tolylhydrazine, to one or more in tolylhydrazine and adjacent tolylhydrazine; Solvent described in activator is alcohols and/or water, preferred C1 ~ C6 alcohol and/or water, comprises one or more in methyl alcohol, ethanol, propyl alcohol, butanols, amylalcohol and hexanol, one or more most preferably in methyl alcohol, second alcohol and water; Described hydrazine class compound accounts for 5% ~ 30% of described activator total mass, and preferably 10% ~ 20%.
Described phthalocyanine catalyst be selected from that metal phthalocyanine, sulfonated metal phthalocyanine derivative and metal gather in phthalocyanine compound one or more.Described metal phthalocyanine catalyst is selected from one or more of Cobalt Phthalocyanine, phthalocyanine vanadium, CuPc, FePC, manganese phthalocyanine and Nickel Phthalocyanine; Described sulfonated metal phthalocyanine derivative catalyst is selected from one or more of sulfonated phthalocyanine cobalt, sulfonated phthalocyanine vanadium, sulfonated phthalocyanine copper, sulfonated phthalocyanine iron, sulfonated phthalocyanine manganese and sulfonated phthalocyanine nickel; Described metal gathers phthalocyanine catalyst and is selected from one or more of poly-Cobalt Phthalocyanine, poly-phthalocyanine vanadium, poly-CuPc, poly-FePC, poly-manganese phthalocyanine and poly-Nickel Phthalocyanine.
The phthalocyanine catalyst used in the present invention directly can add in reactor and carries out sweetening reaction, also can by its load on the framework materials such as gac, atlapulgite and aluminum oxide, then this load phthalocyanine catalyst is joined in reactor carry out sweetening reaction.
Described oils refer to the petroleum products that crude oil is produced through the process such as distillation, catalytic cracking, thermally splitting, hydrocracking, hydrofining and petroleum coking, common example comprise obtain through above-mentioned technique gasoline, diesel oil and kerosene etc.
Described reactor can be intermittent reaction container, also can be continuous reaction container, and preferred fixed-bed reactor, are most preferably provided with the fixed-bed reactor of beds.
The add-on of described activator is 1 ~ 20 μ l/L of described oils cumulative volume, preferably 2 ~ 10 μ l/L;
The add-on of described catalyzer is 0.01 more than μ l/L of described oils cumulative volume, preferably 0.01 ~ 100 μ l/L, most preferably 0.05 ~ 20 μ l/L;
In described oxygen or air in oxygenous and oils the mol ratio of mercaptan between 0.5: 1 ~ 20: 1, preferably 0.5: 1 ~ 15: 1, most preferably 1: 1 ~ 10: 1;
Temperature of reaction between 20 DEG C ~ 80 DEG C, preferably 30 DEG C ~ 70 DEG C, most preferably 40 DEG C ~ 60 DEG C;
Reaction times between 0.01h ~ 10h, preferred 0.02h ~ 8h, most preferably 0.1h ~ 5h; In fixed-bed reactor, calculate by the cumulative volume of the load phthalocyanine catalyst placed in bed, the volume space velocity of oils is 0.1 ~ 100h
-1, preferably 0.125 ~ 50h
-1, most preferably 0.2 ~ 10h
-1.
Reaction pressure is 0.1 ~ 4MPa, preferably 0.1 ~ 3MPa, most preferably 0.1 ~ 2MPa;
The preferred version of inventive desulfurization alcohol method comprises the following steps:
1) load phthalocyanine catalyst is loaded in fixed-bed reactor;
2) activator and oxygen are injected pending oils;
3) by having injected the oils of activator and oxygen in step 2 by being equipped with the fixed-bed reactor of load phthalocyanine catalyst, carrying out sweetening reaction, and collecting the oils after mercaptan removal.
The inventive method mercaptan removal is effective, does not cause secondary pollution to gasoline, without the discharge of waste lye, and has simple to operate, that cost of investment is low advantage.
Embodiment
Material used in the present invention is as follows:
The manufacturer of activator methyl hydrazine, hydrazine hydrate and unsymmetrical dimethyl hydrazine is Chemical Reagent Co., Ltd., Sinopharm Group, analytical pure;
Three kinds of catalyst activity charcoal load sulfonated phthalocyanine cobalts, activated carbon supported poly-Cobalt Phthalocyanine and activated carbon supported sulfonated phthalocyanine nickel using in embodiment are all from Tangshan activated-carbon catalyst company; Wherein catalyzer sulfonated phthalocyanine cobalt accounts for 0.02% of the overall total mass of activated carbon supported phthalocyanine catalyst, catalyzer gather that Cobalt Phthalocyanine accounts for the overall total mass of activated carbon supported phthalocyanine catalyst 0.02%, catalyzer sulfonated phthalocyanine nickel accounts for 0.02% of the overall total mass of activated carbon supported phthalocyanine catalyst;
Catalytically cracked gasoline is Shijiazhuang Oil Refinery MIP gasoline.
In embodiment, the measuring method of mercaptan is potentiometric titration, and method standard is GB/T1792-88.
Embodiment 1
Be 80% by methanol quality content, methyl hydrazine mass content be 20% activator inject containing mercaptan be the catalytically cracked gasoline of 120mg/L, activator injection rate accounts for 3 μ l/L of catalytically cracked gasoline, inject the oxygen with theoretical amount 6 times of volumes needed for catalytically cracked gasoline mercaptan generation complete reaction wherein again, reactor is fixed-bed reactor, its volume is 400ml, aspect ratio is 12: 1, the activated carbon supported cobalt sulfonated phthalocyanine of 200ml is enclosed in reactor, it is 40 DEG C in temperature, under pressure 0.1MPa, with unidirectional flow pump, the catalytically cracked gasoline injecting activator and oxygen is sent into reactor with the flow velocity of 1200ml/h and carry out sweetening reaction, after mercaptan removal, in catalytically cracked gasoline, the content of mercaptan is 4mg/L, still there is activity after running 360h.
Embodiment 2
Be 85% by quality content, hydrazine hydrate mass content be 15% activator inject containing mercaptan be the catalytically cracked gasoline of 120mg/L, activator injection rate accounts for 4 μ l/L of catalytically cracked gasoline, inject the oxygen with theoretical amount 8 times of volumes needed for catalytically cracked gasoline mercaptan generation complete reaction wherein again, reactor is fixed-bed reactor, its volume is 400ml, aspect ratio is 12: 1, the activated carbon supported poly-phthalocyanine cobalt catalyst of 200ml is enclosed in reactor, it is 60 DEG C in temperature, under pressure 0.1MPa, with unidirectional flow pump, the catalytically cracked gasoline injecting activator and oxygen is sent into reactor with the flow velocity of 900ml/h and carry out sweetening reaction, still there is activity after running 360h.After doctor process, in catalytically cracked gasoline, the content of mercaptan is 2mg/L.
Embodiment 3
Be 87% by ethanol mass content, unsymmetrical dimethyl hydrazine mass content be 13% activator inject containing mercaptan be the catalytically cracked gasoline of 120mg/L, activator injection rate accounts for 2 μ l/L of catalytically cracked gasoline, inject the oxygen with theoretical amount 4 times of volumes needed for catalytically cracked gasoline mercaptan generation complete reaction wherein again, reactor is fixed-bed reactor, its volume is 400ml, aspect ratio is 12: 1, enclosing the activated carbon supported sulfonated phthalocyanine nickel catalyzator of 200ml in reactor, is 30 DEG C, pressure 0.1MPa, volume space velocity 6h in temperature
-1carry out sweetening reaction under condition, volume space velocity calculates by the ratio of the cumulative volume of the activated carbon supported sulfonated phthalocyanine nickel catalyzator placed in volumetric flow rate and the bed of catalytically cracked gasoline.After doctor process, in catalytically cracked gasoline, the content of mercaptan is 6mg/L.
Embodiment 4
Be 80% by methanol quality content, methyl hydrazine mass content be 20% activator inject containing mercaptan be the catalytically cracked gasoline of 120mg/L, activator injection rate accounts for 3 μ l/L of catalytically cracked gasoline, inject the oxygen with theoretical amount 6 times of volumes needed for catalytically cracked gasoline mercaptan generation complete reaction wherein again, reactor is fixed-bed reactor, its volume is 400ml, aspect ratio is 12: 1, the activated carbon supported cobalt sulfonated phthalocyanine of 200ml is enclosed in reactor, temperature be 40 DEG C, under pressure 0.1MPa, volume space velocity 30h
-1carry out sweetening reaction under condition, volume space velocity calculates by the ratio of the cumulative volume of the activated carbon supported cobalt sulfonated phthalocyanine placed in volumetric flow rate and the bed of catalytically cracked gasoline.After doctor process, in catalytically cracked gasoline, the content of mercaptan is 20mg/L.
Claims (18)
1. remove a method for mercaptan in oils, be made up of following steps:
Under the existence of phthalocyanine catalyst and oxygen or air, by activator and oils contact reacts in the reactor, collect product; Described activator is the mixture of hydrazine class compound and solvent.
2. in accordance with the method for claim 1, it is characterized in that, described hydrazine class compound is selected from the alkyl derivative of hydrazine, hydrazine hydrate and/or hydrazine.
3. in accordance with the method for claim 2, it is characterized in that, the alkyl derivative of described hydrazine is selected from C1 ~ C5 alkyl hydrazine and/or C1 ~ C5 alkyl substituted benzene hydrazine.
4. in accordance with the method for claim 1, it is characterized in that, described solvent is alcohols and/or water.
5. in accordance with the method for claim 1, it is characterized in that, described solvent is C1 ~ C6 alcohol and/or water.
6. in accordance with the method for claim 1, it is characterized in that, described hydrazine class compound accounts for 5% ~ 30% of described activator total mass.
7. in accordance with the method for claim 1, it is characterized in that, described hydrazine class compound accounts for 10% ~ 20% of described activator total mass.
8. in accordance with the method for claim 1, it is characterized in that, the add-on of described activator is 1 ~ 20 μ l/L of described oils cumulative volume.
9. in accordance with the method for claim 1, it is characterized in that, described phthalocyanine catalyst be selected from that metal phthalocyanine, sulfonated metal phthalocyanine derivative and metal gather in phthalocyanine compound one or more.
10. in accordance with the method for claim 1, it is characterized in that, the add-on of described phthalocyanine catalyst is 0.01 more than μ l/L of described oils cumulative volume.
11. in accordance with the method for claim 1, it is characterized in that, the add-on of described phthalocyanine catalyst is 0.01 ~ 100 μ l/L of described oils cumulative volume.
12. in accordance with the method for claim 1, it is characterized in that, described oils comprises gasoline, diesel oil, kerosene.
13. in accordance with the method for claim 1, it is characterized in that, in described oxygen or air in oxygenous and oils the mol ratio of mercaptan between 0.5: 1 ~ 20: 1.
14. in accordance with the method for claim 1, it is characterized in that, described catalytic temperature of reaction is between 20 DEG C ~ 80 DEG C.
15. in accordance with the method for claim 1, it is characterized in that, the described catalytic reaction times is between 0.01h ~ 10h.
16. in accordance with the method for claim 1, it is characterized in that, described catalytic pressure is 0.1 ~ 4MPa.
17. in accordance with the method for claim 1, it is characterized in that, described phthalocyanine catalyst is the load phthalocyanine catalyst of load on gac, atlapulgite and/or alumina backbone material, described contact reacts is loaded in fixed-bed reactor by load phthalocyanine catalyst to carry out Continuous Contact reaction, calculate by the cumulative volume of the load phthalocyanine catalyst placed in bed, the volume space velocity of oils is 0.1 ~ 100h
-1.
18. in accordance with the method for claim 17, it is characterized in that, the volume space velocity of oils is 0.125 ~ 50h
-1.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2783439C1 (en) * | 2022-02-21 | 2022-11-14 | Публичное акционерное общество "Татнефть" имени В.Д. Шашина | Set for purifying petroleum from hydrogen sulphide and low molecular weight mercaptans |
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| CN104593043B (en) * | 2013-10-30 | 2016-05-25 | 中国石油化工股份有限公司 | The method of condensate deodorization |
| CN105567302B (en) * | 2014-10-17 | 2018-06-19 | 中国石油化工股份有限公司 | A kind of Light Oil Deodorization Method without using inorganic base |
| CN105562091B (en) * | 2014-10-17 | 2018-03-20 | 中国石油化工股份有限公司 | Method for the catalyst aid composition and mercaptan catalyst oxidation of mercaptan catalyst oxidation |
| CN105567303B (en) * | 2014-10-17 | 2017-05-24 | 中国石油化工股份有限公司 | Method for extraction and desulfurization of light hydrocarbon stream |
| CN107445373B (en) * | 2016-05-31 | 2020-04-03 | 中国石化工程建设有限公司 | Treatment process of MTO alkaline washing waste alkali liquor |
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| GB763625A (en) * | 1953-02-06 | 1956-12-12 | Gelsenberg Benzin Ag | Improvements in or relating to the purification of hydrocarbons |
| US4048097A (en) * | 1976-02-19 | 1977-09-13 | Uop Inc. | Sulfonated metal phthalocyanine catalyst |
| CN1048543A (en) * | 1989-05-08 | 1991-01-16 | 美国环球油品公司 | The no caustic alkali sulfur method of sour hydrocarbon stream |
| CN1200956A (en) * | 1997-06-04 | 1998-12-09 | 中国石油化工总公司 | Mercaptan oxidation catalyst and preparation therefor |
-
2011
- 2011-09-29 CN CN201110290862.9A patent/CN103031141B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB763625A (en) * | 1953-02-06 | 1956-12-12 | Gelsenberg Benzin Ag | Improvements in or relating to the purification of hydrocarbons |
| US4048097A (en) * | 1976-02-19 | 1977-09-13 | Uop Inc. | Sulfonated metal phthalocyanine catalyst |
| CN1048543A (en) * | 1989-05-08 | 1991-01-16 | 美国环球油品公司 | The no caustic alkali sulfur method of sour hydrocarbon stream |
| CN1200956A (en) * | 1997-06-04 | 1998-12-09 | 中国石油化工总公司 | Mercaptan oxidation catalyst and preparation therefor |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2783439C1 (en) * | 2022-02-21 | 2022-11-14 | Публичное акционерное общество "Татнефть" имени В.Д. Шашина | Set for purifying petroleum from hydrogen sulphide and low molecular weight mercaptans |
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